Manufacture of sulphuric acid



3 Shee ts-S heet 1 W. F. LAMOREAUX MANUFACTURE SULPHURIC ACID Filed May 29 uor //7/e/ MaiZZ, 1923.

\ mummyayzz, 1923. 1,456,065

: W. F. LAMOREAUX MANUFACTURE OF SULPHUR 1C ACID Filed May 29, 1922 3 Sheets-Shae N? I is? W Edd Nd EHH FE a M -m N 2: a P Q N Q f Wm.-

May 22,1923. 1,456,0 5

w. F. LAMOREAUX MANUFACTURE OF SULPHURIC ACID I Filed May 29, 1922 3 Sheets-Sheet new and useful Im irovementsinthe Mann-f facture of Sulphuric Acid, of which the fol- =tovver may or Patented May 22, 1923. I

winner! I. "risiuoiimux or ISABELIJA, ,TENNluaenn.

- MANUFACTURE or 'sonrnosxe ACID.

4 Application filed May' 29, 192?. 'Serial No. 564,454.

To aZZwfiomz'tma-y concern;

Be it known that I, W L IA F. LAMO unisex, citizen of theUnited States, residing at Isabella, in the county-of Folk and State of Tennessee, have invented certain lowing is :1 Specification.

This invention relates, to an improved process or method of producing sulphuric acid from sulfur dioxidobtained from the burning of elemental sulfur, or from oxides of sulfur such as'are contained in variableadminture with air in-the gases generated,

by'or liberated from any furnace smelting,

roasting, orcalcining pyrite oresor' other sulfur bearing materials.

My invention further relates to'improvements in the apparatus which is'used in the manufacture of "sulphuric acid and -especially to the supplementing ot' the usual chamhers and towers, or indeed the substitution therefor, with apparatus such as will increase the quantity of acid'producedwm a given amount ofreaction' space and in a given interval of time and with a less amount of labor and materials, this being accomplished by the introduction of mechanical means for inducing and maintain-. -by.the reaction 2SO +D :2SO a large It is aning a rapid and constant intensive commingling of the acid making materials thereby providing for a rapid and thorough bringin: into contact of the mol'ecules of all of the reacting fluids both gaseous and-liquid,

' as will be hereinafter more fully set forth in such manner as may be clearly understood and practiced by those versed-in the manufactulge of sulphuric acid.

In the prior art of sulphuric 'acid manufacture there is found no disclosure of any method of producing strong sulphuric acid (that is. acid containing more than 90. per

. cent or" H SQQ hydirect chemical reaction,

except. tl'irough the use of solid catalytic agents=-such as platinum, or iron-oxide. All other methods have comprised the use of evaporation 'efi'ects obtained in concentrating towers or other vessels, wherein the weaker acid is subjected to heatsufiicient to elevate the acid to its boiling point, or distillation temperature, and whereby the acid may be finall v concentiiated to a strength of approximately ninety-eight per cent of H 80 attainment.

The object of my present invention is to produce directly by chemical reaction sulphuric acid of 60 de rees Baum strength r (77.61pm centI-LS or higher degree,

without the use of any solid catalytic agent and without the use ofextraneous heat. I

In my invention, the customary Glover ay not be used, as in any-particular case seems most desirable, but/I prefer to not use the Glover tower except in such cases where the manufactured acid m ust. be quite entirely free f a dissolved i-nltrogen. compou d a 1. my invention'p ties of nitrogen, either in gaseous form or dissolved in sulphuric agents than otherwise,

in the form of sodium nitrate or nitric acid. "wlnch may be introduced directly into the reaction apparatus which I employ.

In-the formation of sulphuric anhydrid amount ofheat is liberated. exothermic reaction and, in accordance with the well known laws of physical chemistry, such reaetions' are quantitatively augmented by the withdrawal or removal of such liber- "ated heat substantially as soon as formed.

If thisheat is not withdrawn, the reactions. are retarded'and never attain quantitative completion. To remove or dissipate the.

acid are used as the oxidizing agents, 211- 7 th'ough they function more as catalytic, or i pseudo-catalytic, *since the oxygen required for formation of heat of reaction there are employed in. thechamber'proce'ss large leaden chambers to provide adequate area of surface for radi- /ation of the heat to the outer'atmosphere,

fc'ontact, or catalytic, processes of sulphuric acid "manufacture, elaborate and costly heat-exchangers or other means of but this .object is always far from perfect Similarly, in the so-called cooling the reactin ases have to be. pro-' n vided, My invention comprises the instant and simu'ltaneousabsorption of the heat by providing intimate contact of the 'gases (having low specific heats) with the cooled liquids (having comparatively higher specific heat-s) which are continuously cooled and circulated in large volumes through the acid-making apparatus which it employ.

in certain other processes for the manufacture of sulphuric. acid the sulfur dioxide is brought into contact with large volumes of nitrous vitriol (nitroso-sulphuric acid or HSNOQ in such quantity that the power of the nitroso-sulpluiric acid to oxidize the S0 is maintai ed unconditiouall v,that is, so that there is no nitrososulphuric acid in the plant which is so w alt as to he inactive for the oxidation of the sulfur dioxide. in such processes it is necessary to keep the strength of the nitrososulphuric acid within certain limits. in order that on the one hand sutlicient water for quick reaction may be present in the acid and on the other hand the capacity of the acid to contain nitrous gases and take up nitrous gases that have been liberated may nevertheless be preserved. In my invention, these limitations are not necessarily imposed, for I cause the S0, laden gases to enter the reaction apparatus wherein, in counter-flow direction. there is introduced strong nitroso-sulphuric acid or nitrous vitriol. which in its downward How is progressively and continuously denitrated by the ascending sulfur dioxide. in this manner the gases rich in sulfur dioxide are brought into contact with the acid containing the minimum quantity of nitrogen oxides and the gases containingthe already largely depleted SQ, content.- are brought in contact with the maximum quantity of nitrogen oxides. Through reaction with the sulfur dioxide such nitrogen oxides as may he liberated in the lower part of the reaction apparatus are in part re-absmhed in the upper levels of the apparatus and descend again into the reaction zone. Home of the nitrogen oxides are, however. not re-ahsorbed in this apparatus. and that these oxides may and shall be absorbed and thus recovered for rc-usc. a second unit oihp paratus provided for this purpose.

The ahove described n'iethod oi operation is the. one which I. generally prefer to use but I have commonly employed the method in which the reacting tluids, both gaseous and liquid, are caused to" flow in the same direction throu h the acid-making apparatus and l do not, therefore, v\'*ish to restrict my invention to the first method alone but rather to include hoth methods. either. of which may he employei'l without departing from my invention.

-Throughout these reactions there is maintained. a deficiencyof water, such as would otherwise be necessary forthe formation of H 590 and consequently practically only sulphuric anhydrid {$3 produced and liberated-in gaseous form, and since the terraces strengths of the acid in the first and second units of my apparatus are not suitable for the quantitative absorption of the sulphuric anhydrid thus formed (nor is it intentional or necessary that they should be), the sulphuric anhydrid is conducted to the .third unit of apparatus containing sulphuric acid of such strength that all of the sulphuric anhydrid is completely absorbed therein.

ln the chamber process of manufacturing sulphuric acid, whenever there occurs a deficiency of water, a large quantity of nitroso-sulphuric acid will be left 'undecomposed and by excessiveconcentration of the acid accumulating in the bottoms of the chambers the nitrogen compounds will be retamed in solution, thus removing them from the atmosphere of the chambers and so losing their aid in oxidizing the sulfur dioxide; but in my present invention this undesirable condition is avoided, or rather advantage is taken of the solubility of these nitrogen compounds in sulphurieacid. for the sulfur dioxide is caused to react directly with these nitrogen compounds while retained in solution.

In all chemical. reactions involving either homogeneous or heterogeneous equilibria, it is known through the well established laws of physical chemistry that the removal of the products of reaction substantially as soon as formed will augment the further reaction otthe remaining components. Advantage of this law is taken in my present invention through the continuous and concurrent removal of the sulphuric anhydrid sul'istantially as soon as formed thus accelerating and augmenting the reaction between the sulfur dioxide and oxygen; this reaction. as previously stated, being brought about through the intermediary, or pseudo-. catalytic. agency 01' the nitrogen compounds present in the gaseous atmosphere, or in solution in the circu ating nitro-sulphuric acid.

lit is a further well known Fact that catalytic, or pseudo-catalytic, action is closely associated with the phenomena oi adsorption and, in turn, the latter phenomena may he rationally considered as manifestations of surface phenomena which are closely akin to the forces of adhesion. An extremely suhdivided phase possesses a relatively large surface compared with the mass of the substance and in applying myresearches to the investigation of these p enomena as pertaining to the manufacture of sulphuric acid, I have discovered that solutions of the nitrogen oxides in sulphuric acid (forming the s -called nitroso-sulphuric acid) may he mp oyed as a catalytic agent for the reaction 2SO,+O :2SO,, provided that the nitrososulphurio acid is subdivided to an extremely high degree of dispersion. Such a high degree of dispersion may he attained bythe meansdescribed in my 'co-pending "plication (Serial No. 492,673 filed Aug, 16th,

1921) and by maintaining the strength or specific gravity of the nitroso-sulphuric 'acid at such a degree that there is never present, in proportion to the sulfur dioxide which is oxidized to sulfur trioxide, a suliicient amount of water directly to form sulphuric acid, then, in that event the sulphuric lanhydrid formed will not be absorbed in the nitroso-sulphuric acid but will .be liberated into the gaseous phase whence it may be removed by the gas stream and subsequently absorbed in strong sulphuricacid.

In theabove manner the acid used for absorbing the sulphuric anhydrid "would continuously increase in strength due to the solution of the SO, but to overcome this, wealra-citl obtained from the first unitis continuouslyadded so that the strength of the absorbing acid is maintained. at any predetermined degreeby these means. The strength of the absorbing acid should pref- 'era-bly bekept at (0,)" about 97 to 99 per actions are as thoughthe'ieaction was from which it will be seen that the nitrososulphuric acid (HSNOQ acts as the catalyt c, or pseudo-catalytic, agent through the intermediary of which the'oxidation of the sulfur dioxide is effected.

' It will be observed from the-above equation that the nitroso-sulphuric acid constitutes a liquid phase and that in the gaseous phase, two molecules of SO unite with one molecule of O to produce two molecules of S0,, therefore, there occurs a shrinkage of oneth rd in the combined volume of the reactdug E50 and 0 Which dictates the reduction ct temperature and increase of pressure in order to augment'the rate of reaction, therefore, these two variables are, at all times,

kept superinduced and under careful control.

' The production 0f high l P Q 0f ,diately or simultaneously causing the disliquids and gases by the method as herein described. enables me to use a considerable pressure throughout the system, such pressure, as, above pointed out, enhancing the reactions. Such pressure may be many times greater than can be used in ordinary lead chambers. For example, I have used pres-- sure up to 16 pounds absolute pressure, and

reac es this pressure may be increased to the extentthat economical operation will warrant.

In principle, in my invention. the rapid oxidationof sulfur dioxide appears to be brought about in the, following manner; \Vith the extreme dispersion of the nitrososulphuric acid in the form of very fine spray or mist there is presented to the gases an enormous extent of liquid surface area thereby inducing such active adsor'ition phenoinena' that large volumes oi. bot SO and become adsorbed or concentrated upon the surfaceiof the liquid and react toform SO,

through the medium of the nitroso-sulplnu'ic acid; but when the minute particles of liqu'id are subsequently coalesced and gatbered into larger masses the adsorption power of the liquid is at once greatly reduced and it no longer capable of retaining the S0,,tl1e latter, therefore, escapes into the gaseous phase to be caried away in the gas stream, and ,finally to be absorbed and retained in concentrated sulphuric acid.

Having described the nature of the reactions believed to'take place in the manufacture of sulphuricanhydrid according to my invention, and furthermore having shown or indicated wherein and whereby these reactions can be accelerated or augmented, I w ll now disclose several methods of acomplisi ing these desired ends, namely by producing the greatest possible area of reacting surface between the gaseous and liquid reagents, which method comprises the high degrees-t dispersion of the liquid phase within that of the gases, and also comprises the high degree of dispersion of the gaseous phase within that of the liquid.

To obtain this high degree of dispersion of the gaseous and liquid phases within each other respectively, I may employ any one of the Well known'rotary or centrifugal. types of gas washer'slsuch as the Fcld washer of vertical type, or the Theisen washerof horizontal type ;indeed, any type of apparatus that will produce such .-a state of high dispersion as to present the/maximum area of reacting surface between the and liquids may be used to carry out the purpose of my invention but it IS quite essential that 4 with whatever type of apparatus that may be used there shall be effected a continuously proceeding method of dispersing the liquid phase components in order to produce newly formed surface films for the absorption oi the gaseous phase components and immematically in the accompanyingdrawings, 7

forming part of this specification, wherein Figure I is a section through one form of apparatus for finely subdiyiding liquid and bringing the particles into contact with the gases,

Figure 11 shows one arrangement of plant wherein the usual type of Glover tower may be used.

Figure III shows a modified arrangement of plant wherein no Glover tower is used.

Inthe accompanying drawing (Figure I), I have chosen the Fold washer to illustrate one type of well known and commercially used apparatus which I have successfully employed in carrying out my invention, but I do. not wish to limit my invention to this particulartype of apparatus or mechanism.

The Feld washer consists of a number of separate ashing chambers 20, mounted one above the other. The ports or openings 21 in the bottom of each chamber act as passages tor the ascending as well as overflows for the counter-current flow of the liquid. The vertical sha'i't 22 suspended from a self-centering, tlIliIl-flK'tlOll bearing 23 is provided in each chamber with a series of concentric trustums of cones it. The

number of cones varies with the size of the- 'through the outer perforated distributing cone." Additiomgl impetus is given the liquid at this point by the greater rim speed ol' the distrilm tor. and the liqu d is projected through the gas space in the Form of line. high velocity spray. which. upon impact with the shell. is still further broken up into a mist or log. thus producing a. very high dispersion oi the liquid absorb iug-medium. and through which. and in intimate contact therewith. the gases are compclled to pass. There is also a continuous circulation ot'liquid within each 'ashing chamhergaml verticali downward from one chamber to another. v

4 Furthermore the violent agitation ol the liquid within each chamber of this apparatus causes an enforced entrainment of the reacting gases within the circulating liquid medium. In other words. by the violent agitation of the liquid the reacting gases are dispersed in the form ot minute hubbles. thus obtaining a dispersion of the aseous phase within that oi the liquid. This is evidenced by the fact that immediately upon discontinuance of the agitation it will be found that the liquid eit'ervesces due to the escape of the minute gas bubbles. These combined methods of dispersion, namely, (a) that of the liquid )hase within the gaseous one and, {5) the ispersion of the gaseous phase Within that of the liquid, together with the alternating humidifying and scrubbing efiect to which the gases are subjected in each chamber, provides a means of enforcingthe intimacy of contact and the extended area of reacting surface between gases and liquid necessary to aceelcrate and augn'ient the chemical reactions involved in the manufacture of sulphuric acid according to my invention.

In F i g'ure II, I. have illustrated one of the ways of carrying my invention into effect, in which particular case the usual type of (Hover towermay be used. The more es-- scntial pieces of apparatus comprise (a) the reaction apparatus 4, wherein the sulfur dioxide is oxidized to sulfur trioxide. or sulphuric anhydrid. through the intermedi ary agency of the oxides of nitrogen and n'troso-sulphuric acid; (b) the apparatus '10 wherein the nitrogen oxides which are set free in washer 4 are subsequently absorbed and recovered this apparatus serving to perform the reactions usually accom plished by means at the well known Gaylaissac. towers. and (c) the sulphuric anhydrid is absorbed and recovered in solution by concentrated sulphuric acid as will he presently more clearly explaimed. In th s same drawing (Figure. the letter A designates the main flue conveying the sulfur-bearing gases from the furnace or roasting apparatus to the Glover tower which may be of usual construction designated by the numeral 1. In the flue. A is usuallybuilt the nit'rati'ng apparatus for enerating the nitric acid and oxids of nitrogen required in the subsequent oxidizing reactions. these compounds mixing with the sulfur dioxide prior to entrance into the bottom of the Glover tower. From the (ilover lower 1-. the gases are drawn through the pipe B by means of the centrifugal tan or pressure blower and are in turn forced into the Fold washer r apparatus 4. From the washer 4. the res dual gases (composed principally of nitrogen. oxygen. nitrogen oxides and sulphuric anhydrid) pass through the washer 14 wherein the sill" phurc anhydrid is entirely absorbed and recovered. From washer 14. the residual *gases,substantially free from all valuable nitrogen and sulfur compounds, escape to the atzi ospliere through the exit pipeiF. By means of-the compressed air system 'G and H, the several acid-ciroulating systems are operated according to the usual practice in acid manufacture ;thus, the denitratd and concentrated acid (of approximately 60 found necessary to maintain the strength of \sulfur. trioxide, or sulphuric anhydrid,

degree Bauin' gravity) from the Glovet' tower 1 is; collected and cooled in the tanki? '2 andby means of the nionteju 3 is pumpedi, to tank 17 in such quantities as may be the acid ,in tank 17 atapproximately ninetyseven to ninetynineipercentsulphuric acid; and from tank 17 the concentrated sulphuric acid flows to and through the washer 14 wherein. the sulphurcanhydrid' is 'abstrengt sorbed and thence intotank 15 where the acid is cooled by rneansof suitable cooling or refrigerating coils, and from tank 15 the acid flows to the montejus 16 to be again pumped to tank 17 for re-circulation. In the process of absorbing' the sulphuric anhydrid, the' acid circulating through the washer 14Qtends to increase in strength and I unless recaution be taken 3 to Prevent the iiof the acid becoming: greater than 97 to 99 per cent H 80 its absorption power,-'that is, for "retaining sulphuric anhydrid, -rapidly decreases, and for this reason the weaker acid from tank 2 is continuously added. (or water or steam may instead be added by means of the pipe W) "to continuously dilute the acid in tank 17 so that its strength may he kept at any predetermined degree, preferably between 97 ,ie 99 per cent H SO or to contain more than 27 per cent free S0,, as has been already explained. In proportion to the accumulation of the strong acid formed by f absorption of sulphuric a-nhydrid in the washer 14,.the amount in excess of the requirement'sfor absorption purposes is drawn "my process.

ofi' into tank S. this acid represents the current production of sulphuric acid made by From time to time. either con tinuously or interm ttently. as operating conditions may determine a portion of concentrated acid from tank 17 is perm tted to flow over to tank 18, thence flowimc through washer 10, to admix' with the weaker acid therein and so increase its strength in order. a that it may be mantained at approximately -59 to '61 degrees Baum. this strength he- 'fing best adapted to the rapid and complete absorption of gaseous oxides of nitrogen. From Washer 10. the acid is collected and gcooled in tank 11 and thence by means of monteju 12 is pumped to tank 13 for recirculation through washer 10. As and when i the circulated acid in tank 13 becomes sufficientlysaturated with oxides of nitrogen, thus forming, the so-called nitroso-sulphuric acid, or "*nitrous vitriol, portions of this a; uitrmisl'vitriol are withdrawn from'tank 13 to tank 9 and caused to admix with the weaker nitrous vitriol which is meanwhile circulating through the Foldwasher or reaction apparatus 4; by this means the strength or-nitrosity of this circulating vitriol is kept at a predetermined strength I pro ortionalto the flaw andftenor of the sul ur dioxide which enters the reaction apparatus 4, and at the same time there is precluded a sufficient quantity (or differently stated,--there is maintained a deficient quantity) of water to unite with the formed; whereas if suiiicient water were otherwise present,- it would unite with the anyhydrid directly to form sulphuric acid. The nitr'osity of the admixed acids from tanks 9 and 7 is so apportioned that the acid flowing from the reaction apparatus 4 into the, cooling tank 5 may or shall'have been,

by reaction with sulfur dioxide, completely for a finished marketable product which may be delivered to tanks, although a por-. tion of th s acid is usually returned back to the acid making system through montejus 3 to tank 17 and 'thusto'resume the cyclic order of performance as described above. In case more intensive'reactions are desired to be brought about in the reaction apparatus 4, additional reagents in the form of nitric acid or other sources of nitrogencornpounds may be added through pipe N, quite independently of, or to supplement. the amount of such nitrogen compounds concurrently ,intro duc ed through the Glover tower '1.

In II I', Ihave illustrated another way of circulating the acid liquids such as may be employed in carrying out my invention without the use of a Glover tower. The essential pieces of apparatus-comprise (a) the reaction apparatus 4, (b) the apparatus 11) for absorption of the nitroaen'oxides; and (n) the apparatus-14 for theahsorption of sulphuric anhydrid; in, each case ie apps ratus chosen for the purpose of illustration consists of a Feld Washer and each of which functions in the manner previously described. in this same drawing (Figure HI) the letter B designate), the main fine conveying the sulfur-bearing gases from the furnace or roasting apparatus to the centrifugal fan (I, through and by means of map which the gases are forced into the Feld washer or apparatus 4-in case, however, the temperature of the gases is too high for practicable operation of the centrifugal fan C, when placed as thus showin then in that event it may be located between the re action apparatus 4 and the absorption apparatus 10, and in this way the temperature of the gases will be sutiicicnfly reduced during their passage through the reaction apparatus i so that they will have no harmful effect upon the fan. in the reaction apparatus the sulfur-dioxide contained in the entering gases is oxidized to sult'ur trioxidc,

or' sulphuric anhyrid, through the intermediary agency of the oxides of nitrogen and nitroso-sulphuric acid which are simultaneously circulated. through this apparatus 4.- From the latter, the gases (consisting 2i} principally of nitrogen, oxygen oxides of nitrogen and sulphuric anhydrid) pass through the pipe I) to the vFeld washer or apparatus 10 where the nitrogen compounds are absorbed. From the washer 10, the remaining gases pass through the pipe E to the apparatus 14 wherein the sulphuric anhydrid is entirely/ absorbed and recovered. From the washer 14, the residual gases cscape to the atmosphere through exit pipc I By means of the compressed air system (land H, the several acid-circulating sys- ,tems are operated according to usual practice in acid manufacture. Through the pipe there is continuously or intermittently led into tank 7 a supply of nitric acid. solution of sodium nitrate, or otlicr sourccs oi" nitrogen compounds which by reaction with the sulphuric acid that is maintained 'in circulation through the apparatus 4 will produco thosenitrogen compounds of suitable quality and in adequate quantities to act as the intermediary,or pscudo-catalyric, agents for the oxidation, oi sulfur dioxide in accordance with the purposes of my invention, as hereinbct'o're set forth. Tlie supply oi nitrogen compounds thus added to the acidmaking system through the pipe N is ordinarily that required to make up any depletion that. normally occurs through the loss ill) ing so regulated that the nitrosity of the vitriol entering the top of the reaction apparatus 4 is at all times kept definitely proportioned to the amount of sulfur dioxide to be. oxidized and, at the same time, so apportionedthatthe acid flowing from the reaction apparatus 4 into the cooling tank 5 shall have been completely, or almost wholly, dcnitrated by reaction with the at all times the strength or gravity of the nitroso-sulphuric acid maintained at. or adjusted to, such a degree that in proportion to the amount of'rlo converted. into S0 there is never present an adequate amount of water to combine with all of the of these compounds; the amount added belatter anhyd rid and thus form H SO .-consequcntly the Flt) remains in the anhydrid form; all of these reactions being controlled principally lay manipulation of the volumes, temperature, and gravity of the circulating acid which caused to pass through the re action ap iaratus. It will also he nnderstood that the gases-richest in sulfur dioi do and oxygen entering through the gas inlet ii are brougl'it into contact with dcnitrated 7 sulphuric acid but, as they ascend'through the reaction apparatus, they come into contact. with nitrous vitriol oi gradually increasing strength, and through reaction with the sulfur dioxid such nitrogen odds as are liberated in the lower parts of the reaction apparatus are in'turn partly reabsorbed in the upper levels and. again descend into the reaction zone in a continuously repeated cyclic order ;.s"ine oi these nitrogen oxides are, however, not absorbed in this a 'iparatus but are carried by the gasstreain into the absorption apparatus 10. From the tank 12h continuous flow oi' su phuri acid (preferably of 59 to ('30 degree llaui'ne gravity) is circulated through this absorption apparatus which absorbs and re tains the nitrogen oxides in solution or con bincd chemically therewith. in the term of nitroso-sulphuric acid, or nitrous vitriol; the latter thence flowing into the cooling tanlt ll to be pumped by means of the monteju 12 to the tank 13, to be re-circulated through the absorption apparatus 10. As and when the acid in tank 13 becomes suitticiently saturated with oxides of nitrogen, portions at this nitrous vitriol are transferred to tank 9 for use in the reaction apparatus 4. During the progress of operations, the acid in circulating through tinabsorber 10 tends to gradually decrease in gravity due to dilution by water, or Water vapor, contained in the gases; and to counteract this effect of dilution (which if not cm'rected would decrease the absorption power of the acid) concentrate-(lucid from .tanlcs 17 and 18 is added in such quantities that the admixed acids are maintained at a gravity of approximately 59 to til degrees launu'a lhrough the absorption appa- 1 ratus l-l there is continuously circulated sul phuric acid of any predetermined strength (but preferably oi 97 to 99 per cent l d 55G; content) whit-h acts as the sulphuric a11- hydrid absm'ption-agentz circulation being clic -tcd by means of the rnonteju 16 as shown. Due to the absorption of 39 the strength of this acid tends continuously to increase, and to correct and control the strength to a predetermined degree there is continuously introduced into the tinixing ta'ulr 17 the required proportion 'oi" weaker and denitrated acid. obtained \from the tank 5; (or water, or steam may beadded 1.10

by means ofthe pipe W). in proportion to the accumulation of the strongacid formed by absorption of sulphuric anhydrid in the apparatus 14, the amount in excess of the requirements for absorption purposes is drawn oil into tank S, this acid represents the current production of sulphuric acid made by my process. i

It will be understood thatv the general arrangement of apparatus shown in Figures H and Ill are only two methods of carrying out my invention by means of a- Well knou'nand commercially used type of gaswasher, and I do not Wish to limit my inrention to this particular arrangement of apparatus or to thisparticular type of apparatus or mechanism,

B 1 means of these acid-circulating systems. the proper quantities and qualities of circulating acids cooled to the proper Working temperatures, can be'easily kept under control so as to maintain a uniformity of quantitative and qualitative factors throughout the whole cycle of the chemical reaction; for, owing to the rapid circulation of both the gaseous and the liquid materials and the conveniently afforded means of regulating the quantities of these materials in varying proportion to each other, faulty conditions of operation can be promptly ascertained and corrections as promptly made, this elasticity of'control being of the greatest importance in the manufacture of sulphuric acid. i I

My process is adapted for use in producing sulphuric acid from sulfur-dioxide laden gases, such as are obtained by burn"- iug sulfur or pyrites, or as lay-products fromroasting or smelting furnaces, or from other sources.

I claim:

l. In a process of oxidizing sulfur dioxide to sulfur trioxide in presence of water, the method comprising dispersing the liquid phase into the gaseous phase. the amount of water present being iusullicicnt to. unite with the whole of the sulfur trioxide resulting from the oxidation.

2. in a process of oxidizing sulfur dioxide to sulfur trioxide in presence of water, the method comprising dispersing the liquid phase into-the gaseous phase. in presence of. a catalyst lhe amount of water present being insuflicient to unite with the whole of the sulfur trioxide resulting from the oxidation. I

3. In a process (if oxidizing sulfur dioxide to sulfur 'trioxide in PlGf-llfit't of: u'atcr. the method comprising dispersing the liquid phase into the gaseous phase. in presence of an oily-nitrogen catalyst, the amount of Water presentbeing insutiicient to unite with the. Whole of the sulfur trioxide resulting from the oxidation.

- s. In a. process of making sulphuric acid by oxidation to S03 in presence of H O, the method of accelerating the reactions between liquid andgaseous phase components,

which consists in dispersing the liquid phase into the gaseous phase and re-collecting the same, said liquid phase containing insufiicient H O to react with the Whole of the-S0 resulting from the oxidation.

5. In a process of making sulphuric acid by oxidation to $0 in presence of H 0 the method of accelerating the reactions between liquid and gaseous phase components, which consists in alternately and repeatedly dispersing the liquid phase into the gaseous phase and re-collecting the same, said liquid phase containing insufficient H O to react with the whole of the S0 resulting from the oxidation.

6. The method of oxidizing S0 to SO which comprises bringing a. gas mixture containing sulfur dioxide and oxygen into contact with nitroso-sulphuric acid. in a state of extreme dispersion, whereby S0 action between the liquid phase, which comprises an oxy-nitrogen catalyst and. the gaseous S0 containing phase, which consists in continuously and so highly dispersing the liquid phase as to presentlthe maximum area of reacting and adsorbing surface between the and liquid, the liquid containing insufficient water to react with the whole of the sulfur trioxideresulting from the reaction, and recovering sulphuric an hydrid from the stream of gases.

8. A process as claimed in claim 7 includ .ing the step 0t removing the heat of reaction by continuously circulating and cooling the liquid.

5). The method of making sulphuric. acid which comprises subjecting the gases formed by the method of claim 7, said gases containing sulphuric anhydrid and nitrogen oxides, to intimate reaction with highly dispersed sulphuric acid of about 60 degrees Baum. in liquid phase. and then absorhing the purified sulphuric anhydrid in concentrated acid of about 98 per cent H 50 content.

10. The method as claimed in claim 9 in which the sulphuric anhydrid is brought into intimate molecular contact with highly dispersed concentrated sulphuric acid.

11. A sulphuric acid plant comprising a reaction apparatus, an apparatus for ab- 's liberated and absorbing sorbing nitrous oxides, and an npparafiw apparaiii s and to the first absorption appafonabsnrbirzg sul 'iiim'icunhydrid, e: ch aplaws, for woling and circulating the liquids pm'atus having means for mechanically pruilierethz'ough. 10 ducing an excemlingiy high dispersion of In testimony wherecf, I affix my signau liquids into the gas stream, means fol pzusscum.

ing the gases through the apparatus in se- 'ries, and means connecied to the mactimi WM.I*.LAMOREAUX. 

